CN202594884U - Equipment for recycling phosphorization cleaning water - Google Patents
Equipment for recycling phosphorization cleaning water Download PDFInfo
- Publication number
- CN202594884U CN202594884U CN 201220088023 CN201220088023U CN202594884U CN 202594884 U CN202594884 U CN 202594884U CN 201220088023 CN201220088023 CN 201220088023 CN 201220088023 U CN201220088023 U CN 201220088023U CN 202594884 U CN202594884 U CN 202594884U
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- exchanger
- water
- rinse water
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Abstract
The utility model relates to the technical field of water circulation treatment equipment, in particular to equipment for recycling phosphorization cleaning water. The equipment comprises a desilicication adsorption exchanger, a strong-acidity cation exchanger, a dephosphorization ion exchanger and a strong-basicity anion exchanger which are connected sequentially. According to the equipment, the desilicication adsorption exchanger can remove silicic acid ingredients from the cleaning water under the action of physisorption; the water produced by the strong-acidity cation exchanger is converted into a diluted inorganic acid mixed solution; the dephosphorization ion exchanger can adsorb a large amount of phosphoric acid under the condition of acidity; and all acidic substances in acidic water are absorbed by the strong-basicity anion exchanger. By the equipment, the conductivity of the product water can be stabilized to be below 5 microseconds/centimeter, the total dephosphorization amount is high, and the amount of discharged total phosphorus is reduced substantially.
Description
Technical field
The utility model relates to water cycle treatment facility technical field, refers in particular to a kind of phosphatization rinse water and recycles treatment facility.
Background technology
In the handware application treating processes, the bonderizing operation that is absolutely necessary.Contain pollution factors such as phosphorus and heavy metal in the phosphatization rinse water that produces in this operation.At present usually with this rinse water and other factory effluent mixed collections; In the collection process through the mutual dilution conduct between the various waste water; The concentration of pollutent phosphorus is reduced; Part enterprise makes the content of phosphorus be reduced to below the emission standard directly discharging through diluting effect, also has part enterprise further to carry out precipitation process and reaches emission standard and discharge later on.
Because with phosphatization rinse water and other factory effluent mixed collections, even carry out precipitation process, deviate from the phosphorus total amount and also reduce greatly, even the concentration of phosphorus reaches emission standard in the draining, but the total phosphorus quantity of discharging also fails to reduce significantly.
Therefore, recycle the defective of treatment process, need recycle treatment process to existing phosphatization rinse water and improve based on above-mentioned existing phosphatization rinse water.
The utility model content
The purpose of the utility model is that the deficiency to prior art provides a kind of phosphatization rinse water to recycle treatment facility, and this phosphatization rinse water recycles treatment facility and solved existing phosphatization rinse water to recycle treatment process existing: deviate from phosphorus total amount total phosphorus quantity few, discharging and defective such as fail to reduce significantly.
For realizing above-mentioned purpose, the utility model is realized through following technical scheme:
The phosphatization rinse water recycles treatment facility, comprises the desiliconization absorption interchanger, strongly acidic cation exchanger, dephosphorization ion-exchanger, the strong-base anion exchanger that connect successively.
Said desiliconization absorption interchanger front end has char filter.
Load strongly acidic cationic exchange resin in the said strongly acidic cation exchanger.
Be filled with the dephosphorization weakly base resin in the said dephosphorization ion-exchanger.
Load strongly basic anion exchange resin in the said strong-base anion exchanger.
Use the micro-content organism impurity that exists in the char filter absorption rinse water in the conceptual design, the replacement cycle of gac is directly related with the organic content in the rinse water, can reach more than half a year at least according to the engineering experience replacement cycle.
Preparation pure water process using the level Four ion exchange treatment, the first step is handled and has been adopted desiliconization absorption interchanger, is filled with the blended polymeric adsorbent in the interchanger.Usually contain silicofluoric acid in the phosphatization rinse water, decomposition reaction can all take place in silicofluoric acid when PH is greater than 3.5, generate hydrofluoric acid and colloid silicic acid.Concrete decomposition is reacted as follows:
H
2SiF
4+H2O→H
2SiO
3+HF+H
+
Colloid silicic acid will have a strong impact on the carrying out of IX desalinating process, therefore must at first use the special-purpose polymeric adsorbent of desiliconization that colloid silicic acid is adsorbed to deviate from.This adsorption process is a physical adsorption process, can reply its adsorptive power through the mode of using soda acid alternately to clean after resin absorption is saturated.
Second stage ion-exchange unit has adopted strongly acidic cation exchanger.Rinse water gets into after this grade equipment, and following chemical exchange reaction takes place for all positively charged ions in the rinse water and resin:
R-H+M
+→R-M+H
+
R represents ion exchange resin in the formula, M
+Represent the various positively charged ions in the water, the result of permutoid reaction is that the whole positively charged ions in the water all are transformed into H
+, rinse water changes into very rare inorganic acid solution.Need after resins exchange is saturated to use acid solution to regenerate.
Third stage ion-exchange unit has adopted the dephosphorization ion-exchanger.Contain a large amount of phosphate anions in the rinse water, and the exchange capacity of common anionite-exchange resin is lower, the cycle of operation of anion exchanger will not shorten greatly when not using the dephosphorization ion-exchanger.Selected dephosphorization weakly base resin is very big to the exchange capacity of phosphate radical, can prolong the cycle of operation of whole plant.Concrete chemical exchange reaction is:
R-OH+H
2PO
4 -→R-H2PO4+OH
-
R represents ion exchange resin in the formula, and permutoid reaction is replaced the OH that gets off
-Ion immediately with water in H
+Ionic bond forms water molecules, and the phosphate compsn of rinse water is just deviate from like this.
2H
++OH
-→H2O
Need after resins exchange is saturated to use sodium hydroxide solution to regenerate.
The fourth stage has adopted strong-base anion exchanger.Rinse water gets into after this grade equipment, and following chemical exchange reaction takes place for all negatively charged ion in the rinse water and resin:
R-OH+A
-→R-A+OH
-
R represents ion exchange resin in the formula, A
-Represent various other negatively charged ion in the water, the result of permutoid reaction is that the whole negatively charged ion in the water all are transformed into OH
-, permutoid reaction is replaced the OH that gets off
-Ion immediately with water in H
+Ionic bond forms water molecules, and all impurity of rinse water are just deviate from like this.Need after resins exchange is saturated to use sodium hydroxide solution to regenerate.
The impurity that is dissolved in the water after handling through above-mentioned level Four will all be deviate from, and the product electrical conductivity of water can be stablized and reaches below the 5 μ S/cm.
The beneficial effect of the utility model is: at first with the organic additive in the char filter absorption rinse water, then through desiliconization absorption interchanger; In desiliconization absorption interchanger, be filled with the blended polymeric adsorbent, can pass through physisorption, remove the silicic acid component in the rinse water; Through strongly acidic cation exchanger, in this equipment, positively charged ion in the rinse water and resin carry out ion exchange reaction to rinse water after the desiliconization again, and all positively charged ion changes the hydrogen ion of equivalent into, produce water and change into very rare mineral acid mixing solutions; Sour water through the dephosphorization ion-exchanger, is filled with elite weakly basic anion exchange resin earlier in this interchanger, under acidic conditions, can adsorb a large amount of phosphoric acid; At last through the whole acidic substance in the strong-base anion exchanger absorption sour water, the product electrical conductivity of water can be stablized and reaches below the 5 μ S/cm, deviates from phosphorus total amount total phosphorus quantity many, that discharge and reduces significantly.
Description of drawings
Fig. 1 is the catenation principle synoptic diagram of the utility model.
Embodiment
Below in conjunction with accompanying drawing the utility model is further described.
See Fig. 1; The phosphatization rinse water of collecting at first need be removed suspended particle wherein; Because of the phosphatization rinse water water yield generally can be very not big; Therefore can directly use fine and close deep bed filter to carry out filtration treatment, the general requirement filtering accuracy reaches below the 25um, and the deep bed filter filtration capacity of selecting for use should reach more than 3 times of the actual treatment water yield.
Rinse water after the filtration is carried out adsorption treatment through char filter 1, and the filtration capacity of char filter 1 is generally pressed 8m
3/ m
2Design, the backwash cycle of char filter 1 generally is designed to 12 hours, prevents that carbon leaching material from hardening.
After this phosphatization rinse water need be passed through the level Four purifying treatment.Be filled with the blended polymeric adsorbent in the first step treatment facility desiliconization absorption interchanger 2, the filler loadings generally is controlled at below 2/3 of strainer cubic capacity, and filtration capacity is generally pressed 10m
3/ m
2Design.
Load strongly acidic cationic exchange resin in the second stage treatment facility strongly acidic cation exchanger 3, the filler loadings generally is controlled at below 2/3 of strainer cubic capacity, and filtration capacity is generally pressed 12--15m
3/ m
2Design.
The elite acidulous anion exchange resin of filling in the third stage treatment facility dephosphorization ion-exchanger 4, the filler loadings generally is controlled at below 2/3 of strainer cubic capacity, and filtration capacity is generally pressed 12--15m
3/ m
2Design.
Load strongly basic anion exchange resin in the fourth stage treatment facility strong-base anion exchanger 5, the filler loadings generally is controlled at below 2/3 of strainer cubic capacity, and filtration capacity is generally pressed 15--20m
3/ m
2Design.
Regeneration system rapidly can be designed as downflow system regeneration, also can be designed to reverse-flow regeneration, and wherein reverse-flow regeneration can be practiced thrift regenerant consumption.
The regeneration water is taken from the water that self produces of native system, and regenerative wastewater is carried out sneaking into after the precipitation process and carried out qualified discharge in other waste water.
The utility model can be realized recycling of phosphatization rinse water with phosphatization rinse water single collection through treatment facility.Can reduce the enterprise wastewater total emission volumn through this treatment facility, can with the pollution factor enrichment method in the phosphatization rinse water in regenerative wastewater, be convenient to further carry out precipitation process simultaneously, help reducing gross contamination emission.
Certainly; The embodiment of the above; It is the preferred embodiments of the utility model; And unrestricted the utility model practical range, so all equivalences of doing according to the described structure of the utility model claim, characteristic and principle change or modify, all should be included in the utility model claim.
Claims (5)
1. the phosphatization rinse water recycles treatment facility, it is characterized in that: comprise the desiliconization absorption interchanger, strongly acidic cation exchanger, dephosphorization ion-exchanger, the strong-base anion exchanger that connect successively.
2. phosphatization rinse water according to claim 1 recycles treatment facility, it is characterized in that: said desiliconization absorption interchanger front end has char filter.
3. phosphatization rinse water according to claim 1 recycles treatment facility, it is characterized in that: load strongly acidic cationic exchange resin in the said strongly acidic cation exchanger.
4. phosphatization rinse water according to claim 1 recycles treatment facility, it is characterized in that: be filled with the dephosphorization weakly base resin in the said dephosphorization ion-exchanger.
5. phosphatization rinse water according to claim 1 recycles treatment facility, it is characterized in that: load strongly basic anion exchange resin in the said strong-base anion exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220088023 CN202594884U (en) | 2012-03-09 | 2012-03-09 | Equipment for recycling phosphorization cleaning water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220088023 CN202594884U (en) | 2012-03-09 | 2012-03-09 | Equipment for recycling phosphorization cleaning water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202594884U true CN202594884U (en) | 2012-12-12 |
Family
ID=47312442
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220088023 Expired - Fee Related CN202594884U (en) | 2012-03-09 | 2012-03-09 | Equipment for recycling phosphorization cleaning water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202594884U (en) |
-
2012
- 2012-03-09 CN CN 201220088023 patent/CN202594884U/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20121212 Termination date: 20150309 |
|
| EXPY | Termination of patent right or utility model |